|Publication number||US4954561 A|
|Application number||US 07/373,925|
|Publication date||Sep 4, 1990|
|Filing date||Jun 30, 1989|
|Priority date||Jun 30, 1989|
|Also published as||CA2020149A1, EP0405608A2, EP0405608A3|
|Publication number||07373925, 373925, US 4954561 A, US 4954561A, US-A-4954561, US4954561 A, US4954561A|
|Inventors||Richard M. Gerkin, John F. Timberlake|
|Original Assignee||Union Carbide Chemicals And Plastics Company Inc.|
|Export Citation||BiBTeX, EndNote, RefMan|
|Patent Citations (12), Referenced by (8), Classifications (11), Legal Events (13)|
|External Links: USPTO, USPTO Assignment, Espacenet|
1. Field of the Invention
The present invention relates to stabilizers for polymer/polyols, their preparation, the polymer/polyols so produced employinq the stabilizer and polyurethane foams made from such polymer/polyols. More particularly, the instant invention relates to stabilizers made from N-(polyoxyalkyl)-N-(alkyl)amines and bi-functional unsaturated monomers.
2. Description of the Prior Art
Polymer/polyol compositions suitable for use in producing polyurethane foams, elastomers and the like are known materials. The basic patents in the field are Stamberger U.S. Pat. No. Re. 28,715 (reissue of U.S. Pat. No. 3,383,351) and U.S. Pat. No. Re. 29,118 (reissue of U.S. Pat. No. 3,304,273). Such compositions can be produced by polymerizing one or more ethylenically unsaturated monomers dissolved or dispersed in a polyol in the presence of a free radical catalyst to form a stable dispersion of polymer particles in the polyol. These polymer/polyol compositions have the valuable property of imparting to polyurethane foams and elastomers produced therefrom higher load bearing properties than are provided by the corresponding unmodified polyols.
The polymer/polyol compositions that found initial commercial acceptance were primarily compositions produced using acrylonitrile. Many of these compositions were somewhat higher in viscosity than desired in some applications. More recently, polymer/polyol compositions produced from acrylonitrile styrene monomer mixtures have been used commercially.
Polyurethane foams made with polymer/polyols are widely utilized. The two major types of foam are generally termed slabstock and molded. More particularly, slabstock foams employing polymer/polyol compositions are used in the carpet, furniture and bedding industries. One primary use of slabstock foam is as carpet underlay.
In the molded foam area, the primary type of foam employed is generally termed high resiliency (HR) molded foam. HR molded foams have been widely used in the automotive industry for applications ranging from molded seats to energy-absorbing padding and the like.
The wide demand for polymer/polyols has spawned a number of trends that have created the need for additional technology. For example, the general trend is to provide slabstock foams that are virtually scorch free, i.e., white foam products. Indeed, the desire is to provide techniques capable of producing, without substantial economic penalty, virtually scorch free foams at ever decreasing densities (viz.--1.5 pounds per cubic foot or less) while maintaining satisfactory load-bearing and other foam properties.
Such scorch-free foams have been obtained by utilizing relatively high styrene contents (e.g. --about 65 to 70 percent styrene) in the acrylonitrile-styrene monomer mixture. The utilization of such high styrene monomer mixtures in the molded foam area is also widespread.
The preparation of polymer/polyols from such high styrene monomer mixtures has created difficulties. More particularly, such difficulties arise due to the state of the art to which polyurethane production has now advanced, such as the degree of the stability of polymer/polyol compositions. Many applications require somewhat rigorous stability characteristics, and such characteristics become more difficult to achieve when high styrene monomer mixtures are employed.
A further trend is the desire to provide foams with ever-increasing load bearing characteristics for many applications. This is particularly prevalent in the slabstock area where many formulations require the use of "neat" polymer/polyols, i.e., the polymer/polyol is employed without dilution with conventional polyols. While typically not used neat in the molded foam area, polymer/polyols capable of imparting higher and higher load-bearing characteristics to such foams are likewise desired.
Such increased load-bearing characteristics are being obtained by increasing the polymer or solids content of the polymer/polyol. Solids contents of 35 to 50 weight percent or even more are accordingly desired. Preparing such high solids content polymer/polyols with the degree of stability often desired becomes substantially more difficult as the solids content is increased.
The trend toward the use of high styrene monomer mixtures and high solids content polymer/polyols has likewise resulted in polymer/polyols sometimes having higher than desired viscosities. The viscosity of a polymer/polyol must, of course, be sufficiently low to allow ease in handling during manufacture. Moreover, the viscosity must allow ready transport, handling and, ultimately, adequate processability in the foam processing equipment being utilized. The viscosity level is becoming of acute concern in the molded area due to the sophisticated mixing systems, such as impingement systems, that are increasingly being utilized. There is a clear need to provide the desired polymer/polyols with as low a viscosity as possible.
Also, the degree of stability of the polymer/polyol, as alluded to previously, is of concern. At one time, there was not much concern for the seediness or filterability of polymer/polyols in actual commercial practice. However, the state of the art of polyurethane production has now advanced to the point where these considerations are very important in many applications. This is particularly important in the molded foam area.
Thus, the development of sophisticated, high speed and large volume equipment, machines and systems for handling, mixing and reacting polyurethane-forming ingredients has created the need for highly stable and low viscosity polymer/polyols. Polymer/polyols must accordingly meet certain minimum requirements in order to be capable of being satisfactorily processed in the sophisticated foam equipment now used. Typically, the prime requirement is that the polymer/polyols possess sufficiently small particles so that filters, pumps and the like do not become plugged or fouled in relatively short periods of time.
Since the basic development by Stamberger, a substantial amount of effort has been devoted to providing improved polymer/polyols and to improved preparation techniques. For example, U.S. Pat. No. 4,208,314 to Priest et al. discloses low viscosity polymer/polyols made from acrylonitrile styrene monomer mixtures. These polymer/polyols can be converted to low density, water-blown polyurethane foams having reduced scorch, especially when the acrylonitrile-to-styrene ratio is relatively low. The Priest et al. patent also provides a process for making polymer/polyols whereby the particulate nature of the polymer portion of the product is considerably improved, compared to polymer/polyols prepared by prior processes. The improved process provided by Priest et al. includes, in general, maintaining a low monomer to polyol concentration throughout the reaction mixture during the polymerization.
A further improvement in the formation of polymer/polyols is provided by U.S. Pat. No. 4,148,840 to Shah. This discloses a process for producing highly stable and filterable polymer/polyol compositions by polymerizing the monomer or monomers in situ in a polyol mixture that includes a minor amount of preformed polymer/polyol.
It has been recognized that the stability of polymer/polyols requires the presence of a minor amount of a graft or addition copolymer which is formed in situ from growing polymer chains and polyol molecules. Some prior approaches have thus been directed to incorporation of small amounts of unsaturation into the polyol in addition to that inherently present in the polyoxyalkylene polyols typically used in forming polymer/polyols in the belief that improved stability will result due to an increased amount of an addition copolymer stabilizer expected to be formed. U.S. Pat. Nos. 3,652,639, 3,823,201, and 3,850,861, British Patent No. 1,126,025 and Japanese Patent Nos. 52-80919 and 48,101494 all utilize this approach.
In a similar vein, the use of what may be termed "stabilizer precursors" has been proposed. More specifically, the concept is to carry out the preparation of the polymer/polyol in the presence of a suitable amount of the stabilizer precursor, which precursor comprises what has been termed a "macromer" that contains a particular level of reactive unsaturation. The belief is that, during polymerization in the preparation of the polymer/polyol, adequate amounts of stabilizer will be formed by the addition polymerization of the precursor stabilizer with a growing polymer chain. The concept of using stabilizer precursors in polymerization is a well-recognized and old technique as discussed in "Dispersion Polymerization in Organic Media", edited by K. E. J. Barrett, John Wiley & Sons, copyright 1975. U.S. Pat. Nos. 4,454,255 and 4,458,038 are recent examples utilizing this technique. The macromer in the '255 and '038 patents may be obtained by reacting a polyol with a compound having reactive ethylenic unsaturation such as, for example, maleic anhydride or fumaric acid. A further example of the use of this technique is U.S. Pat. No. 4,460,715. The reactive unsaturation in the '715 stabilizer is provided by an acrylate or methacrylate moiety.
More recently, U.S. Pat. No. 4,550,194 disclosed a polyol which is alleged to find utility as a precursor in the preparation of graft polymer dispersions although no specific mention of its use to prepare a stabilizer is made. This polyol is prepared by reacting a conventional polyether polyol with an organic compound having ethylenic unsaturation and an anhydride group forming a half ester and subsequently reacting that product with alkylene oxide in the presence of calcium naphthenate or cobalt naphthenate. In particular, see example 51 of this patent where pentaerythritol is used.
In U.S. Pat. No. 4,652,589 stabilizer precursors are taught for polymer/polyols. In particular, Stabilizers A and B utilized polyols with added unsaturation.
In addition, U.S. Pat. No. 4,390,645 discloses a stabilizer made from a polyahl and isocyantoethylmethacrylate.
Unexpectedly, it has now been found that the combination of an amine terminated polyether and a bifunctional unsaturated monomer produces an unsaturated, amine containing stabilizer which allows for the preparation of superior polymer polyols and foams made therefrom.
The primary object of the present invention is to provide a new stabilizer which will allow for the production of stable polymer/polyols having high polymer contents with low viscosities.
It is another object of the present invention to provide a stabilizer that can be utilized in low levels in producing stable polymer/polyols.
It is yet another object of this invention to provide stable polymer/polyols having small particle size and acceptable particle shape.
Another object of the present invention is to prepare a urethane foam that is characterized as having open cells and whose formulation is stable during its formation so as to avoid foam collapse.
Other objects of this invention will be apparent from the description and examples set forth hereinafter.
This invention deals with the preparation of a stabilizer precursor, hereinafter referred to for brevity as a "stabilizer", the use of such a stabilizer to make an improved polymer/polyol, and the polyurethane foams subsequently prepared from such polymer/polyols which foams show improved properties.
The key feature of the stabilizer are the use of N (polyoxyalkyl)-N-(alkyl)amines and a bi-functional unsaturated monomer.
The stabilizers are then employed in making polymer/polyols by conventional techniques.
The polymer/polyols made utilizing the stabilizers are advantageously employed in making polyurethane foams by conventional techniques. These foams exhibit surprising and improved foam properties, i.e., open foams which are more stable during formation.
Suitable stabilizers are, in general, prepared by the reaction of the selected reactive bi-functional unsaturated compound with the selected polyol.
By the terminology reactive bi-functional unsaturated compound, it is meant any compound capable of forming an adduct with an amine terminated polyether, either directly or indirectly, and having carbon-to carbon double bonds which are adequately reactive with the particular monomer system being utilized. More specifically, compounds containing alpha, beta unsaturation are preferred. Suitable compounds satisfying this criteria include maleic anhydride, maleates, fumarates, acrylates, and methacrylates. While not alpha, beta unsaturated compounds, amine terminated polyether adducts formed from substituted vinyl benzenes such as chloromethylstyrene may likewise be utilized. Illustrative examples of suitable unsaturated compounds which may be employed to form the stabilizer precursor include 1,1-dimethyl-m-isopropenylbenzyl isocyanate, maleic anhydride, itaconic anhydride, fumaric acid, tetrahydrophthalic anhydride, dialkyl fumarates, dialkyl maleates, glycol maleates, glycol fumarates, isocyanatoethyl acrylate or methacrylate, methyl acrylate or methacrylate, hydroxyalkyl acrylate or methacrylate, acrylic and methacrylic acid and their anhydride, methacroyl chloride and glycidyl methacrylate. The preferred compound is 1,1-dimethyl-m-isopropenylbenzyl isocyanate.
The N-(polyoxyalkyl) N- (alkyl) amine reactant is of the general formula, ##STR1## wherein: R represents an initiator radical based on a compound containing Zerewitinoff active hydrogen atoms;
H represents a hydroxy containing group of the formula: ##STR2## P represents a primary amine containing group of the formula: ##STR3## S represents a secondary amine-containing group of the formula: ##STR4## T represents a tertiary amine-containing group of the formula: ##STR5## a is 0 to 175; b is 0 to 175;
c is 0 to 30;
n is 1 to 3;
the sum a+b+c must be greater than or equal to 2 when n equals 1;
R' is an alkyl group containing from two carbon atoms to eighteen carbon atoms;
R" is hydrogen or an alkyl group containing up to eighteen carbon atoms;
R'" and R"" are independently alkyl groups containing from two to twelve carbon atoms;
p is a mole fraction of the aminated portion of the amine reactant and is from 0 to less than 0.75;
s is a mole fraction of the aminated portion of the amine reactant and is from 0.25 to 1.0;
t is a mole fraction of the aminated portion of the amine reactant and is from 0 to 0.15;
w is the percent amination of the zerwitinoff active hydrogen atoms on the intermediate compound, generally 30 percent to 100 percent, and preferably 70 percent or more.
(zw) is the product of z and w;
z is an inteqer derived from the number of Zerewitinoff active hydrogens on the initiator.
The preparation of such amine terminated polyethers is disclosed in U.S. patent application Ser. No. 176,217 filed Mar. 31, 1988.
The level of retained ethylenic unsaturation in the stabilizer is preferably at least 60% of that initially added to the reactants. It is preferred to prepare the stabilizer in such a fashion that the unsaturation is retained to the maximum extent possible, most preferably above 80%.
Loss of unsaturation may occur in stabilizer preparation with any of the alpha, beta unsaturated compounds. For example, it has been recognized that when maleic anhydride is employed anywhere from about 25 percent to essentially all of the unsaturation may be lost. Loss in unsaturation appears to be generally accompanied by an increase in viscosity of the stabilizer. It is accordingly desirable to utilize an efficient process in the preparation of the stabilizer.
On the other hand, the maximum level of unsaturation is constricted by crosslinking of the stabilizer which may occur. More particularly, when higher levels of unsaturation are attempted to be added in preparing the stabilizer, there is a greater probability that species will be formed having more than one double bond per molecule, i.e., be something other than a monoadduct. An undue population of such specie may cause crosslinking and thus adversely affect the ability of the stabilizer to provide the requisite dispersion stability enhancement, as well as substantially increasing the viscosity. Accordingly, the maximum level of unsaturation added should be below that at which significant crosslinking occurs, that is, on the average no more than about one carbon-to carbon double bond per molecule of stabilizer should occur.
It has been found satisfactory to maintain the ratio of the reactive bifunctional unsaturated compound to amine terminated polyether in the range of from about 0.5 to about 1.5 moles of the reactive unsaturated compound per mole of amine terminated polyether, more preferably 0.7 to about 1.1 mole per mole of amine terminated polyether.
The specific level of unsaturation utilized will further depend on the molecular weight of the amine terminated polyether used to prepare the stabilizer and on the viscosity of the stabilizer itself.
Viscosities of greater than 1500 cks (25° C.) are preferred. The maximum viscosity of useful stabilizer will be typically dictated by practical considerations. More specifically, the viscosity of the stabilizer should not be so high that it cannot be conveniently handled. Viscosities up to perhaps 10,000 to 15,000 cks or so should be capable of being satisfactorily handled. Moreover, by blending with base polyol in the reactor used to form the stabilizer, even substantially higher viscosities (e.g., up to 25,000 to 40,000 cks or higher) should be suitable.
The viscosity can then be increased above 1500 cks by one of two means. The first method is to continue to react (cookout) the stabilizer preparation under the controlled conditions until the desired viscosity is achieved. By this method at least 60% or greater of the added unsaturation is retained depending to some extent on how high the viscosity is raised.
A second method to raise the viscosity, which is preferred because a higher level of added unsaturation can be maintained (60 to 100%) at high viscosities, is to couple the stabilizer with a chemically reactive compound such as polyisocyanate (preferably MDI), dimethyl oxalate, succinoyl chloride and the like to the desired viscosity. Generally, no unsaturation is lost during the reaction of polyisocyanate with the stabilizer.
The polyol or blends thereof, employed as the base polyol depends upon the end use of the polyurethane product to be produced. The molecular weight or hydroxyl number of the base polyol may thus be selected so as to result in flexible, semi-flexible, or rigid foams or elastomers when the polymer/polyol produced from the base polyol is converted to a polyurethane. The hydroxyl number of the polyol or polyols employed can accordingly vary over a wide range. In general, the hydroxyl number of the polyols employed may range from about 20 (or lower) to about 150 (and higher).
For example, when foams are to be prepared, the molecular weight or the hydroxyl number may be selected to result in flexible, semi-flexible, or rigid foams. The polyols in this instance preferably possess a hydroxyl number of at least 150 for rigid foams, from about 50 to about 150 for semi flexible foams, and from about 20 to about 70 for flexible foams. As a further refinement, the specific foam application will likewise influence the choice of base polyol. As an example, for molded foam, the hydroxyl number of the base polyol may be on the order of about 20 to about 40, and for slabstock the hydroxyl number may be on the order of about 25 to about 70.
As a further example, for elastomer applications, it will generally be desirable to utilize relatively high molecular weight base polyols having relatively low hydroxyl numbers, e.g., 20 to 50 or so.
The hydroxyl number limits described above are not intended to be restrictive, but are merely illustrative of the large number of possible combinations for the polyol or polyols used.
The hydroxyl number is defined as the number of milligrams of potassium hydroxide required for the complete hydrolysis of the fully phthalated derivative prepared from one gram of polyol. The hydroxyl number can also be defined by the equation:
OH=hydroxyl number of the polyol
f=functionality, that is, average number of hydroxyl groups per molecule of polyol
m.w.=number average molecular weight of the polyol.
Substantially any of the polyols previously used in the art to make polymer/polyols can be used as the base polyol in this invention. Illustrative of the polyols useful in producing polymer/polyol compositions in accordance with this invention are the polyhydroxyalkanes, the polyoxyalkylene polyols, or the like. Among the polyols which can be employed are those selected from one or more of the following classes of compositions, alone or in admixture, known to those skilled in the polyurethane art:
(a) alkylene oxide adducts of polyhydroxyalkanes;
(b) alkylene oxide adducts of nonreducing sugars and sugar derivatives;
(c) alkylene oxide adducts of phosphorus and polyphosphorus acids;
(d) alkylene oxide adducts of polyphenols;
(e) the polyols from natural oils such as castor oil, and the like.
Illustrative alkylene oxide adducts of polyhydroxyalkanes include, among others, the alkylene oxide adducts of ethylene glycol, propylene glycol, 1,3-dihydroxypropane, 1,3-dihydroxybutane, 1,4-dihydroxybutane, 1,4-, 1,5- and 1,6 dihydroxyhexane, 1,2-, 1,3 1,4-, 1,6-, and 1,8-dihydroxyoctane, 1,10-dihydroxydecane, glycerol, 1,2,4-trihydroxybutane, 1,2,6-trihydroxyhexane, 1,1,1-trimethylolethane, 1,1,1-trimethylolpropane, pentaerythritol, caprolactone, polycaprolactone, xylitol, arabitol, sorbitol, mannitol, and the like.
A further class of polyols which can be employed are the alkylene oxide adducts of the nonreducing sugars, wherein the alkylene oxides have from 2 to 4 carbon atoms. Among the nonreducing sugars and sugar derivatives contemplated are sucrose, alkyl glycosides such as methyl glucoside, ethyl glucoside, and the like, glycol glycosides such as ethylene glycol glucoside, propylene glycol glycoside, glycerol glucoside, 1,2,6-hexanetriol glucoside, and the like, as well as the alkylene oxide adducts of the alkyl glycosides as set forth in U.S. Pat. No. 3,073,788.
A still further useful class of polyols is the polyphenols, and preferably the alkylene oxide adducts thereof wherein the alkylene oxides have from 2 to 4 carbon atoms. Among the polyphenols which are contemplated are, for example, bisphenol A, bisphenol F, condensation productions of phenol and formaldehyde, and novolac resins; condensation products of various phenolic compounds and acrolein; the simplest member of this class being 1,2,3-tris(hydroxyphenyl) propanes, condensation products of various phenolic compounds and glyoxal, glutaraldehyde, and other dialdehydes, the simplest members of this class being the 1,1,2,2-tetrakis (hydroxyphenol) ethanes, and the like.
The alkylene oxide adducts of phosphorus and polyphosphorus acids are another useful class of polyols. Ethylene oxide, 1,2-epoxypropane, the epoxybutanes, 3-chloro-1,2-epoxypropane, and the like are preferred alkylene oxides. Phosphoric acid, phosphorus acid, the polyphosphoric acids such as tripolyphosphoric acid, the polymetaphosphoric acids, and the like are desirable for use in this connection.
Indeed, any material having an active hydrogen as determined by the Zerewitinoff test may be utilized as the base polyol. For example, amine terminated polyether polyols are known and may be utilized, if desired.
The most preferred base polyols employed in this invention include the poly(oxypropylene) glycols, triols, and higher functionality polyols, and the like that are capped with ethylene or propylene oxide as dictated by the reactivity requirements of the particular polyurethane application. Generally, the nominal functionality of such polyols will be in the range of about 3 to 4 or so. These polyols also include poly-(oxypropylene-oxyethylene) polyols; however, desirably, the oxyethylene content should comprise less than 80 percent of the total and preferably less than 60 percent. The ethylene oxide, when used, can be incorporated in any fashion along the polymer chain. Stated another way, the ethylene oxide can be incorporated either in internal blocks, as terminal blocks, or may be randomly distributed along the polyol chain.
As is well known in the art, the polyols that are most preferred herein contain varying small amounts of unsaturation. Unsaturation in itself does not affect in any adverse way the formation of the polymer/polyols in accordance with the present invention except in the case where the extent or type of unsaturation is so high as to result in a highly crosslinked polymer/polyol or gel.
Conceptually, a wide variety of monomers may be utilized in the preparation of the polymer/polyol compositions in accordance with the invention. Numerous ethylenically unsaturated monomers are disclosed in the prior patents. Any of these monomers should be suitable.
The selection of the monomer or monomers used will depend on considerations such as the relative cost of the monomers and the polyurethane product characteristics required for the intended application. To impart the desired load-bearing to the foams, the monomer or monomers used in preparing the polymer/polyol should, of course, desirably be selected to provide a polymer which has a glass transition of at least slightly higher than room temperature. Exemplary monomers include styrene and its derivatives such as para-methylstyrene, acrylates, methacrylates such as methyl methacrylate, acrylonitrile and other nitrile derivatives such as methacrylonitrile, and the like. Vinylidene chloride may also be employed.
The preferred monomer mixtures used to make the polymer/polyol compositions of this invention are mixtures of acrylonitrile and styrene or acrylonitrile, styrene and vinylidene chloride.
As the amount of styrene or its derivatives in the monomer mixture is increased above about 70 weight percent or so, it becomes increasingly more difficult to make satisfactorily stable polymer/polyols. Additionally, at such high styrene levels, problems other than stability are also typically encountered. These problems include a decrease in conversion of the styrene monomer and the concomitant need to adequately strip the styrene monomer, as well as an increase in the viscosity of the polymer/polyol. Despite these drawbacks, levels of styrene greater than 75 weight percent and even as high as 100 weight percent may be desirable.
The monomer content will be typically selected to provide the desired solids content required for the anticipated end-use application. In general, it will usually be desirable to form the polymer/polyols with as high a resulting polymer or solids content as will provide the desired viscosity and stability properties. The present invention is highly desirable for preparing polymer/polyols having solids contents in excess of 10 percent by weight, based upon the weight of the polymer/polyol composition preferably above 25 percent.
For molded foam applications, typically high resiliency formulations, solids content of up to about 45 weight percent or more are feasible and may be provided utilizing the present invention. In slabstock applications, the tendency is to utilize as high a solids content as possible, contents of 45 weight percent to about 50 weight percent or more being desired commercially for some applications.
The polymer/polyols of this invention are produced by polymerizing the monomer system used in the presence of a free radical catalyst in the base polyol and a stabilizer.
The stabilizer, as previously described, should be added to the base polyol in an amount sufficient to provide the desired stability assistance for the resulting polymer/polyol. It will generally be suitable to incorporate a stabilizer in amounts from 1 to about 25 percent or so, based upon the weight of the polyol. Levels from about 3 percent to about 10 percent by weight or are prepared. If desired, a mixture of stabilizers can, of course, be used.
The polymer/polyols of the present invention are preferably prepared utilizing the process set forth in the previously identified Priest et al. patent. In accordance with that process, a low monomer-to-polyol ratio is maintained throughout the reaction mixture during the polymerization process. Such low ratios are achieved by employing process condition that provide rapid conversion of monomer to polymer. In practice, a low monomer-to-polyol ratio is maintained, in the case of semi-batch and continuous operation, by use of a free radical polymerization catalyst, by control of the temperature and mixing conditions and, in the case of semi-batch operation, by slowly adding the monomers to the polyol.
The mixing conditions employed are those attained using a back-mixed reactor (e.g., a stirred flask or stirred autoclave). Reactors of this type keep the reaction mixture relatively uniform and so prevent localized high monomer-to-polyol ratios. However, tubular reactors may be employed if they are modified so that increments of the monomer are added to various stages.
The utilization of the Priest et al. process is preferred since this allows the preparation of polymer/polyols with a wide range of monomer composition, polymer contents, and base polyol that could not be otherwise prepared with the necessary stability now often desired. However, whether the utilization of the Priest et al. process is essential depends upon whether the process parameters are such that a satisfactory polymer/polyol can be prepared without using this process.
Other processing technology is disclosed in the prior art and may likewise be used in the preparation of the polymer/polyols of the present invention. For example, the techniques set forth in U.S. Pat. No. 4,119,586 to Shah may be employed, if desired.
Control of residence time has been found useful in controlling both the degree of crosslinking (XLC) and the intrinsic viscosity of the polymer which, as mentioned in U.S. Pat. No. 4,463,107, may be advantageous. In a continuous operation, a stable dispersion of a polymer in a polyol is produced where the residence time, which is defined as that time calculated by dividing the reactor's volume by the volumetric flow rate of the total feed to the reactor, is from about 1 minute to about 5 hours, and preferably, from about 10 minutes to about 2 hours.
In a semi-batch operation where the reactor can be partially charged prior to initiating polymerization, the term residence time refers to that period of time during which significant polymerization of the monomer or co-monomers occurs. In semi-batch operation, residence times from about 30 minutes to about 10 hours are recommended.
Catalysts useful in producing the polymer/polyol compositions of this invention are the free radical type, vinyl polymerization catalysts such as the peroxides, percarbonates, and the azo compounds. Any other suitable catalyst may be employed. Azo catalysts such as azobis (isobutyronitrile) are the preferred catalysts. 2,2'-azobis (isobutyronitrile) is particularly preferred because it does not increase the acid number of the product, does not impart objectionable odor to the product, and does not require special handling, particularly as compared to certain peroxide catalysts.
The catalyst concentration can be varied within reasonably wide limits. The catalyst concentration will accordingly typically be adjusted to optimize the polymer/polyol properties. Accordingly, the concentration will generally be in the range of about 0.1 to about 3 weight percent based on the total feed to the reactor. The preferred amount of catalyst will be in the range of about 0.2 weight percent to about 1.0 weight percent. Up to a certain point, increases in the catalyst concentration result in increased monomer conversion but further increases do not substantially increase conversion. Conversions of monomers to polymers which can be typically achieved are on the order of 75% to 98% of the monomer charged. On the other hand, increasing catalyst concentration increasingly improves product stability. The catalyst concentration selected will usually be an optimum value considering all factors, including costs.
The temperature used in producing polymer/polyol compositions in accordance with the invention is not in itself critical and can be any temperature at which the selected catalyst has a reasonable rate of decomposition under the reaction conditions. Typically, in continuous processes, reaction temperatures of from about 100° C. to about 150° C. may be used, the preferred range being from about 100° C. to about 125° C. It has been found that with higher reaction temperatures there is a tendency for the intrinsic viscosity of the polymer to decrease. Accordingly, lower temperatures are preferred, typically in the range from about 105° C. to about 125° C.
Further, the addition of a polymer control agent during the polymerization reaction has been found to be useful. In general, as used herein, the terminology polymer control agent connotes a low molecular weight liquid which, upon use in preparing the polymer/polyol, results in polymer structure such that the polymer has low crosslinking coefficient and controlled intrinsic viscosity. Virtually any low molecular weight liquid should be suitable. A variety of low molecular weight carbon-hydrogen compounds are known and may be employed. The suitability of a particular liquid may be readily determined simply by employing the liquid in the polymer/polyol preparation. Accordingly, low molecular weight liquids may be employed regardless of whether any significant chain transfer activity is exhibited.
Low molecular weight liquids not conventionally viewed as chain transfer agents but useful as polymer control agents include water, cyclohexane, and benzene. Suitable polymer control agents which are conventionally viewed as chain transfer agents include ketones, alcohols, aldehydes, halogenated compounds, benzene derivatives and the like.
Any such known chain transfer agents can be utilized as the polymer control agents, if desired.
The polymer control agent or agents used should be added in an amount that will provide a polymer having the desired properties. Suitable levels will, of course, vary as discussed herein. Amounts up to 20 weight percent or higher, based on the total feed to the reactor, may be used satisfactorily. More typically, useful levels will be about 2 to 10 percent or so.
The viscosity of the polymer/polyol compositions can vary over a wide range, depending upon the limitations and requirements of the particular end use application. As a practical matter, it is generally desired to minimize the viscosity for obvious reasons. When the viscosity gets too high, it becomes difficult to handle the polymer/polyol, particularly in off-loading, mixing, and the like. In general, it is desired that the viscosity of the resulting polymer/polyol be less than about 10,000 cks at 25° C.
The viscosity of the resulting polymer/polyols will also typically vary depending upon the intended polyurethane application. In high resiliency molded foam applications where solids contents on the order of 25 to 45 weight percent or so are often used (typically diluted with conventional polyols in commercial formulations), the viscosities of the thus-diluted polymer/polyols will typically be in the 3500 to 5000 cks (25° C.) range or higher. In slabstock applications where solids contents of 35 to 60 percent by weight or more are desired and the polymer/polyols are sometimes used neat, the viscosity will typically be above about 3500 cks (25° C.) or so, often ranging up to 8000 cks (25° C.) or so.
From the functional standpoint, suitable polymer/polyols must be capable of being: (1) made, (2) stored, (3) shipped, and (4) used without undue loss of polymer content or damage or fouling of the equipment in which it is made and handled. If a polymer/polyol meets these functional criteria, it is generally considered to be satisfactorily stable.
The present invention also provides a method for producing polyurethane products which include reacting: (a) a polymer/polyol composition of this invention, and (b) an organic polyisocyanate in the presence of (c) a catalyst for the reaction of (a) and (b) to produce the polyurethane product. When a foam is being prepared, the reaction is carried out in the presence of a blowing agent and a foam stabilizer. The reaction and foaming operations can be performed in any suitable manner, preferably by the one shot technique.
The polymer/polyol may, if desired, be blended with conventional polyols or the like to reduce the polymer content to the level required for the particular end-use application. Blends in which the resulting polymer content is as low as 4 percent of the total weight of the blend, or even less, are useful.
The organic polyisocyanates that are useful in producing polyurethane products in accordance with this invention are organic compounds that contain at least two isocyanato groups. Such compounds are well-known in the art. Suitable organic polyisocyanates include the hydrocarbon diisocyanates (e.g., the alkylene diisocyanates and the arylene diisocyanates), as well as known triisocyanates and polymethylene poly (phenylene isocyanates). Examples of suitable polyisocyanates are 2,4-diisocyanatotoluene, 2,6-diisocyanatotoluene, methylene bis(4-cyclohexyl isocyanate), 1,2-diisocyanatoethane, 1,3-diisocyanatopropane, 1,2-diisocyanatopropane, 1,4-diisocyanatobutane, 1,5-diisocyanatopentane, 1,6-diisocyanatohexane, bis(3-isocyanatopropyl)ether, bis(3-isocyanatopropyl) sulfide, 1,7-diisocyanatoheptane, 1,5-diisocyanato-2,2-dimethylpentane, 1,6-diisocyanato 3-methoxyhexane, 1,8-diisocyanatooctane, 1,5-diisocyanato-2,2,4-trimethylpentane, 1,9-diisocyanatononane, 1,10-diisocyanatopropyl)ether of 1,4-butylene glycol, 1,11-diisocyanatoundecane, 1,12-diisocyanatododecane bis(isocyanatohexyl) sulfide, 1,4-diisocyanatobenzene, 3,5-diisocyanato-o-xylene, 4,6-diisocyanato-m xylene, 2,6-diisocyanato-p-xylene, 2,4-diisocyanato-1-chlorobenzene, 2,4-diisocyanato-1-nitrobenzene, 2,5-diisocyanato-1-nitrobenzene, 4,4-diphenylmethylene diisocyanate (MDI), 2,4-diphenylmethylene diisocyanate, 3,3-diphenyl-methylene diisocyanate, and polymethylene poly (phenyleneisocyanates), and mixtures thereof. Also suitable as the "liquid" derivatives of MDI described in U.S. Pat. No. 3,394,164 and the various prepolymers or quasi prepolymers dervied from either MDI or the liquid version of MDI upon reaction with hydroxyl or amine containing polyethers. The preferred polyisocyanate is about 80% of a mixture of 80% 2,4-tolylene diisocyanate and 20%, 2,6-tolylene diisocyanate and about 20% of a polymeric isocyanate.
Any known catalysts useful in producing polyurethanes may be employed. Representative catalysts include: (a) tertiary amines such as bis(2,2'-dimethylamino)ethyl ether, trimethylamine, triethylamine, N-methylmorpholine, N-ethylmorpholine, N,N-dimethylbenzylamine, N,N-dimethylethanolamine, N,N,N',N'-tetramethyl-1,3-butanediamine, triethanolamine, 1,4-diazabicyclo-[2.2.2]octane, pyridine oxide and the like; (b) tertiary phosphines such as trialkylphosphines, dialkylbenzylphosphines, and the like; (c) strong bases such as alkali and alkaline earth metal hydroxides, alkoxides, and phenoxides; (d) acidic metal salts of strong acids such as ferric chloride, stannic chloride, stannous chloride, antimony trichloride, bismuth nitrate and chloride, and the like; (e) chelates of various metals such as those which can be obtained from acetylacetone, benzoylacetone, trifluoroacetylacetone, ethyl acetoacetate, salicylaldehyde, cyclopentanone-2-carboxylate, acetylacetoneimine, bis-acetylacetonealkylenediimines, salicylaldehydeimine, and the like, with the various metals such as Be, Mg, Zn, Cd, Pb, Ti, Zr, Sn, As, Bi, Cr, Mo, Mn, Fe, Co, Ni, or such ions as MoO2 ++, UO2 ++, and the like; (f) alcoholates and phenolates of various metals such as Ti(OR)4, Sn(OR)4, Sn(OR)2, Al(OR)3, and the like, wherein R is alkyl or aryl, and the reaction products of alcoholates with carboxylic acids, beta diketones, and 2(N,N-dialkylamino)alkanols, such as the well known chelates of titanium obtained by said or equivalent procedures; (g) salts of organic acids with a variety of metals such as alkali metals, alkaline earth metals, Al, Sn, Pb, Mn, Co, Bi, and Cu, including, for example, sodium acetate, potassium laureate, calcium hexanoate, stannous acetate, stannous octoate, stannous oleate, lead octoate, metallic driers such as manganese and cobalt naphthenate, and the like; (h) organometallic derivatives of tetravalent tin, trivalent and pentavalent As, Sb, and Bi, and metal carbonyls of iron and cobalt.
Among the organotin compounds that deserve particular mention are dialkyltin salts of carboxylic acids, e.g., dibutyltin diacetate, dibutyltin dilaureate, dibutyltin maleate, dilauryltin diacetate, dioctyltin diacetate, dibutyltin bis(4-methylaminobenzoate), dibutyltin bis(6-methylaminocaproate), and the like. Similarly, there may be used a trialkyltin hydroxide, dialkyltin oxide, dialkyltin dialkoxide, or dialkyltin dichloride. Examples of these compounds include trimethyltin hydroxide, tributyltin hydroxide, trioctyltin hydroxide, dibutyltin oxide, dioctyltin oxide, dilauryltin oxide, dibutyltin bis(isopropoxide) dibutyltin-bis(2-dimethylaminopentylate), dibutyltin dichloride, dioctyltin dichloride, and the like.
The tertiary amines may be used as primary catalysts for accelerating the reactive hydrogen/isocyanate reaction or as secondary catalysts in combination with one or more of the above-noted metal catalysts. Metal catalysts, or combinations of metal catalysts, may also be employed as the accelerating agents, without the use of amines. The catalysts are employed in small amounts, for example, from about 0.001 percent to about 5 percent, based on the weight of the reaction mixture.
When the product to be formed is a polyurethane foam, a small amount of a blowing agent is employed in the reaction mixture. Suitable blowing agents, for example, include water from about 0.5 to about 5 weight percent, based upon total weight of the polymer/polyol composition, or other suitable blowing agents which are vaporized by the exotherm of the reaction, or a combination of water and the other blowing agent. Illustrative polyurethane blowing agents include halogenated hydrocarbons such as trichloromonofluoromethane, dichlorodifluoromethane, dichloromonofluoromethane, dichloromethane, trichloromethane, 1,1-dichloro-1-fluoroethane, 1,1,2-trichloro-1,2,2-trifluoroethane, hexafluorocyclobutane, octafluorocyclobutane, and the like. Another class of blowing agents include thermally unstable compounds which liberate gases upon heating such as N,N'-dimethyl-N,N'-dinitrosoterephthalamide, amine formates, and the like. The generally preferred method of foaming for producing flexible foams is the use of water, or a combination of water plus a fluorocarbon blowing agent such as trichloromonofluoromethane. The quantity of blowing agent employed will vary with factors such as the density desired in the foamed product.
The scorch-free properties of the foams produced using polymer/polyol compositions are most evident when at least some of the blowing agent is water, and the water is used in an amount that results in a foam having a density less than 3.0 pounds per cubic foot. Generally, the use of water in an amount of about 2.0 percent by weight, based on the total weight of the polymer/polyol composition, results in a foam having a density of less than 3.0 pounds per cubic foot.
It is also within the scope of the invention to employ, when applicable, small amounts, e.g., about 0.001 percent to 5.0 percent by weight, based on the total reaction mixture, of a foam stabilizer. Suitable foam stabilizers or surfactants are known and may vary depending upon the particular polyurethane application. Suitable stabilizers for slabstock applications include "hydrolyzable" polysiloxane-polyoxyalkylene block copolymers such as the block copolymers described in U.S. Patents 2,834,748 and 2,917,480. Another useful class of foam stabilizers are the "non-hydrolyzable" polysiloxane-polyoxyalkylene block copolymers such as the block copolymers described in U.S. Pat. Nos. 3,505,377 and 3,686,254 and British Patent Specification No. 1,220,471. The latter class of copolymers differs from the above-mentioned polysiloxane-polyoxylakylene block copolymers in that the polysiloxane moiety is bonded to the polyoxy-alkylene moiety through direct carbon-to-silicon bonds, rather than through carbon-to-oxygen-to-silicon bonds. These various polysiloxanepolyoxyalkylene block copolymers preferably contain from 5 to 50 weight percent of polysiloxane polymer, with the remainder being polyoxyalkylene polymer. Yet another useful class of foam stabilizer is composed of the cyanoalkyl-polysiloxanes described in U.S. Pat. No. 3,905,924.
The polyurethanes so produced may be utilized in foam and elastomer applications where any conventional type of polyurethane is or can be utilized. The polymer/polyol compositions of this invention find particular utility in the production of high resiliency foams for use in arm rests, mattresses, automobile seats, and the like, as well as in slabstock foams for use as carpet underlayment, and the like.
Whereas the exact scope of the instant invention is set forth in the appended claims, the following specific examples illustrate certain aspects of the present invention and, more particularly, point out methods of evaluating the same. However, the examples are set forth for illustration only and are not to be construed as limitations on the present invention except as set forth in the appended claims. All parts and percentages are by weight unless otherwise specified.
As used in the Examples, the following designations, symbols, terms and abbreviation have the following meanings:
Polyol #1=A polyoxyalkylene oxide hexol produced from propylene oxide and ethylene oxide and sorbitol having an hydroxyl number of ca. 28 mg KOH/g. The ethylene oxide content is 10% by weight, present as an internal block.
Polyol #2=A conventional polyol stabilizer based on Polyol #1 which has been allowed to react with 0.1 meq/g of maleic anhydride followed by ethylene oxide to cap the generated acid.
Polyol #3=A polyoxyalkylene oxide triol produced from propylene oxide and glycering in which the polymerization was run at 105° C. The product has an hydroxyl number of ca. 38 mg KOH/g.
Polyol #4=A polyoxyalkylene oxide triol produced from propylene oxide and glycerine having an hydroxyl number of 240 mg KOH/g.
Polyol #5=A polyoxyalkylene oxide triol made from propylene oxide and ethylene oxide and glycerine with an hydroxyl number of 52 mg KOH/g. The polyol contains 10% ethylene oxide by weight present as an internal block.
Catalyst #1=Commercial catalyst sold by Harshaw/Filtrol Partnership as Ni 5136P.
TMI=1,1-dimethyl-m-isopropenyl benzyl isocyanate.
ATP=amine terminated polyether.
Polyol #1 (78% by wt.), isopropylamine (22% by wt.) and Catalyst #1 (2.5% on polyol) were charged to a high pressure autoclave. The system was pressurized to ca. 100 psi with hydrogen and vented three times to remove air. After pressurizing to 200 psi with hydrogen, the autoclave was sealed and heated to 220° C. for four hours. After cooling, the contents of the reactor were filtered to remove the catalyst, and the remaining volatile amine was vacuum stripped at 120° C. The product had the following analysis: Total amine 0.39 meg/g.; conversion 83%; secondary amine content 22%; primary amine content 78%.
A five gallon autoclave was charged with 1250 g of polyol #4, 1150 g heptane and 7.5 g of zinc hexacyanacobaltate catalyst. The reactor was purged with nitrogen and evacuated to 2 psi at room temperature. The catalyst was activated for 2.5 hr. at 80° C. and 380 g (20 psia partial pressure) of propylene oxide fed. Almost no induction period was observed, and pressure dropped as soon as cook-out began. A total of 20 kg of propylene oxide was fed at a rate of 11800 g/hr. After work up via vacuum stripping to remove volatiles, the polyol had an hydroxyl number of 16.2 mg KOH/g.
Polyol Ex. #2 (1276g), isopropyl amine (201.6 g) and Catalyst #1 (26 g) were added to a high pressure autoclave as described in Ex. #1. After pressurizing to 500 psi, the mixture was heated to 233° C. and held for 8 hr. Filtration and stripping gave a product with the following analysis: Total amine 0.239 meq/g; conversion 83.5%; tertiary amine 0.0005 meq/g; secondary amine content 43.2%; primary amine 56.8%.
The ATP from Ex. #1 (350 g) was added to a flask equipped with an efficient stirrer. IEM (5.425 g, 0.1 meq/g of ATP) was added to the ATP with good stirring. After a small exotherm, the mixture was allowed to react for 1 hr. at ambient temperature. The stabilizer had the following analysis: Total amine 0.316 meq/g; viscosity (Cannon Fenske) 3881 cks.
The ATP from Ex. #1 (350 g) was added to a flask equipped with an efficient stirrer and heated to 70° C. TMI (7.035 g, 0.1 meq/g of ATP) was added and the mixture allowed to stir for 1 hr. at this temperature. The stabilizer had the following analysis: Total amine 0.316 meq/g, viscosity 4008 cks.
The ATP from Ex. #1 (600 g) was added to a flask and heated to 80° C. Maleic anhydride (5 88 g, 0.1 meq/g of ATP) was added and the mixture stirred at this temperature for 1 hr. The stabilizer had the following analysis: Total amine 0.30 meq/g, viscosity 22,308 cks.
Polyol #1 (400 q) was added to a flask and heated to 70° C. IEM (6.2 g, 0.1 meq/g) was added followed by 0.04 g of dibutyltindilaurate catalyst. After 3 hr. at this temperature, the reaction was complete (Infra red analysis). The stabilizer had an hydroxyl number of 22.3 mg KOH/g and a viscosity of 2737 cks.
Polyol #1 (400 g) was added to a flask and heated to 70° C. TMI (8.4 g, 0.1 meq/g) was added followed by 0.04 g of dibutyltindilaurate catalyst. After 3.5 hr. the reaction was complete. The stabilizer had an hydroxyl number of 22.4 mg KOH/g and a viscosity of 3033 cks.
Coupling--The ATP of Ex. #1 (900 g) was added to a flask and heated to 120° C. Diethyl oxalate (4.44 g) was added to the hot ATP and the mixture stirred at this temperature for 3 hr. The ethanol condensate was removed by vacuum stripping to yield a product with an amine number of 0.37 meq/g. This coupled product (650 g) and IEM (10.14 g, 0.1 meq/g) were allowed to react as in Ex. #4 to give a stabilizer with the following analysis: Total amine 0.276 meq/g, viscosity 6456 cks.
Coupling--The ATP of Ex. #1 (600 g) was added to a flask and heated to 120° C. Diethyl oxalate (3.24 g) was added to the hot ATP and the mixture stirred at this temperature for 3 hr. The ethanol condensate was removed by vacuum stripping to yield a product with an amine number of 0.334 meq/g. The coupled product (350 g) and TMI (7.035 g, 0.1 meq/g of ATP) were allowed to react as in Ex. #4 to give a stabilizer with the following analysis: Total amine 0.229 meq/g, viscosity 12,212 cks.
Coupling--The ATP of Ex. #1 (500 g) was added to a flask and heated to 120° C. Diethyl oxalate (1.35 g) was added to the hot ATP and the mixture allowed to stir at this temperature for 3 hr. The ethanol condensate was removed by vacuum stripping to yield the partially coupled product. This material (400 g) and TMI (8.04 g) were allowed to react as in Ex. #4 to give the stabilizer with the following analysis: Total amine 0.261 meq/g, viscosity 9946 cks.
Polyol #1 (3000 g) diisopropylamine (1528.9 g) and Catalyst #1 (105 g) were charged to an autoclave and pressurized to 200 psi with hydrogen. The system was sealed and heated to 190° C. for ca. 16 hr. The mixture was cooled, filtered and stripped to remove excess amine yielding a product with the following analysis: Total amine 0.386 meq/g; conversion 82.6%; secondary amine 75.5%; primary amine 24.5%.
ATP from Ex. #3 (500 g) was added to a flask equipped with an efficient stirrer. IEM (7.75 g) was added to the ATP at 24.5° C. with good stirring, and the mixture allowed to react 1 hr. at this temperature (a slight exotherm was noted on addition). The stabilizer had the following analysis: Total amine number 0.163 meq/g; viscosity 5292 cks.
ATP of Ex. #3 (500 g) was added to a flask equipped with an efficient stirrer and heated to 70° C. TMI (10.05 g) was added with good stirring and allowed to react at this temperature for 1 hr. The stabilizer had the following analysis: Total amine number 0.17 meq/g; viscosity 6216 cks.
ATP from Ex. #12 (400 g) was added to a flask equipped with a good stirrer and heated to 70° C. TMI (8.04 g) was added with good stirring and allowed to react for 1 hr. at this temperature. The stabilizer had the following analysis: Total amine number 0.318 meq/g; viscosity 3642 cks.
Coupling --ATP of Ex. #12 (300 g) was added to a flask and heated to 125° C. with good stirring. Diethyl oxalate (0.47 g) was added and heated continued for 3 hr. at this temperature. The ethanol condensate was stripped under vacuum yielding a product with an amine number of 0.356 meq/g. 200 g of this coupled material was added to a flask and heated to 70° C. with good stirring. TMI (4.02 g, 0.1 meq/g) was added and allowed to react for 1 hr. at this temperature. The stabilizer had the following analysis: Total amine number 0.26 meq/g; viscosity 4722 cks.
Polyol #3 was aminated according to the procedure described in Ex. #1. This ATP had the following analysis: Total amine number 0.45 meq/g; conversion 92%: secondary amine 27%; primary amine 73%.
All polymer polyols were prepared using a single stage 550 ml backmixed continuous reactor with a 20 min. residence time. The reactor was maintained at a temperature of 125° C. and about 45 psi pressure during the entire reaction sequence. The comonomers used were styrene and acrylonitrile at a ratio of 66/34%, wt./wt. The initiator was azo bisisobutyronitrile, used at a level of 0.6% by weight based on the solution in the monomers. The polyol in which the polymerization was carried out was Polyol #5. The stabilizer being studied was added directly to this polyol. The feed rates for the polyol/stabilizer and comonomer/initiator mixtures were approximately 890 and 760 q/hr. respectively. The targeted total solids content for the final product for all runs was 45%. After a suitable line out time (ca. 1 to 2 hr.), material was collected for a total of 180 minutes. This product was then vacuum stripped to remove unreacted monomer and then analyzed. This procedure was used to prepare the polymer polyols described in Examples 18 through 27, and comparative Examples 1, 2 and 3 as shown in Table I.
TABLE 1__________________________________________________________________________Polymer Polyols From Various StabilizersContinuous ProcessStab. from UseEx. #Ex # Type Level Viscosity Part. Size Shape*__________________________________________________________________________18 6 ATP/mal 3% 10,200 cks 3.29 u 319 4 ATP/IEM 3% 10,494 cks 3.7 u 220 5 ATP/TMI 3% 6,099 cks 2.46 u 421 9 cATP/IEM** 3% 9,730 cks 3.01 u 322 10 cATP/TMI 3% 8,444 cks 2.11 u 523 11 pcATP/TMI*** 3% 6,407 cks 2.23 u 524 11 pcATP/TMI 5% 7,180 cks 1.83 u 525 9 cATP/IEM 10% 14,206 cks 1.63 u 526 16 ATP/IEM 3% 17,113 cks 3.16 u 227 17 ATP/TMI 3% 8,588 cks 2.62 u 2Comp.Examples1 8 OH/TMI 3% 5,552 cks 2.85 u 42 8 OH/IEM 3% 6,150 cks 2.79 u 33 Polyol # OH/mal 3% 5,685 cks 2.91 u 32__________________________________________________________________________ *Shape Factor Ratings 1 = Rough, lumpy surface, not round. 2 = Lumpy surface, particle generally round. 3 = Only slightly lumpy, particle round. 4 = Round, fuzzy appearance. 5 = Round, smooth surface. **cATP = coupled stabilizer see example ***pcATP = partially coupled stabilizer see example
A polymer dispersion in the ATP described in Example #17 was prepared according to the following procedure: The ATP from Ex. #17 (468 g) was added to a flask equipped with an efficient stirrer a dropping funnel and a nitrogen source. The stabilizer (if used) was added, and the mixture heated at 125° C. with stirring. Styrene (92.4 g), acrylonitrile (39.6 g) and azo-bisisobutyronitrile (3.74 g, 0.6% on total charge) were mixed and added to the dropping funnel. This monomer mixture was then added slowly to the hot ATP at such a rate as to keep the reaction temperature below about 130° C. After all of the monomer was added, the dispersion was stirred an additional 2 hr. at 125° C. Unreacted monomer was removed by vacuum stripping, yielding the polymer/ATP dispersion. Analyses are given in Table 2.
TABLE 2__________________________________________________________________________Polymer Dispersions in an ATP From Various StabilizersBatch ProcessTot.Ex. # Stab. from Use Part.Amine Ex. # Type Level Viscosity Size Shape*__________________________________________________________________________28 5 ATP/TMI 5% 3,304 cks 0.20 u 50.36129 11 pcATP/TMI 5% 3,310 cks 0.20 u 50.36130 15 ATP/TMI 5% 3,065 cks 0.21 u 50.36531 16 pcATP/TMI 5% 2,962 cks 0.21 u 50.36632 none -- -- 3,212 cks 0.27 u 10.368__________________________________________________________________________ Shape Factor. See Table 1.
TABLE 3__________________________________________________________________________Evaluation of Polymer Polyols Made From Different StabilizersIn A Typical Foam Formulation Compar #4 Compar #5 33 34 35 36 37 38__________________________________________________________________________Foam FormulationPolymer Polyol From: Compar #1 Compar #2 Ex. 4 Ex. 5 Ex. 10 Ex. 9 Ex. 13 Ex. 14Water (php) 2.3 → → → → → → →Catalyst 1** 0.03 → → → → → → →Catalyst 2** 0.10 → → → → → → →Surfactant 1** 0.70 → → → → → → →TDI (Index) 115 → → → → → → →Stabilizer Type: Polyol/IEM Polyol/TMI ATP/IEM ATP/TMI cATP/TMI cATP/IEM ATP/IEM ATP/TMICream Time, sec. 10 11 10 11 10 10 10 11Rise Time 126 150 144 148 119 131 131 151Tightness 53.2 63.7 58.5 66.3 23.1 46.7 49.3 66.3Comments Good Cure Sl. Green Sl. Green Good Good Good Good Sl. GreenFoam Properties*Density, pcf 2.43 24.2 2.42 2.43 2.36 2.41 2.41 2.41Porosity 53.55 65.4 58.9 69.7 26.6 48.2 53.6 69.7IFD-Thickness 4.05 4.05 4.04 4.09 4.02 4.06 4.05 4.05IFD, 25% 139.75 137.0 143.7 143.3 149.5 150.3 134.3 135.3IFD, 65% 309.00 307.5 329.3 328.8 336.3 340.0 310.3 307.0IFD, 25% Return 84.25 81.3 82.6 81.4 86.2 87.1 77.8 78.8Return Value 60.29 59.3 57.4 56.8 57.7 58.0 57.9 58.3IFD 65/25 2.21 2.24 2.29 2.29 2.25 2.27 2.31 2.27CFD, 25% 1.80 1.67 1.74 1.69 1.84 1.86 1.71 1.66CFD, 65% 3.62 3.31 3.51 3.41 3.59 3.77 3.44 3.33Tensile, psi 29.24 27.45 29.5 29.30 34.5 34.7 29.2 30.7Elongation, % 62.3 60.7 59.4 65.1 72.3 72.3 57.9 68.1Tear, pli 1.8 2.26 2.30 2.57 2.94 2.3 2.36 2.40Compress. Set. 90% 7.98 7.10 9.57 8.17 8.06 9.51 9.79 7.52__________________________________________________________________________ *ASTM D3574-77 **Catalyst 1 = Urethane catalyst supplied commercially by UCC as Niax Catalyst A1. Catalyst 2 = Urethane catalyst supplied commercially by UCC as Niax Catalyst D19. Surfactant 1 = A silicone surfactant supplied commercially by UCC as L6202.
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|U.S. Classification||524/728, 252/182.18|
|International Classification||C08F283/06, C08G18/63, C08G18/81|
|Cooperative Classification||C08G18/8108, C08G18/636, C08G18/635|
|European Classification||C08G18/63P, C08G18/63R, C08G18/81B|
|Dec 11, 1989||AS||Assignment|
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Effective date: 19940421
|May 7, 1996||AS||Assignment|
Owner name: HUNTSMAN CORPORATION, UTAH
Free format text: RELEASE OF SECURITY INTEREST;ASSIGNOR:TEXACO INC.;REEL/FRAME:007927/0245
Effective date: 19960129
|Aug 7, 1996||AS||Assignment|
Owner name: HUNTSMAN PETROCHEMCIAL CORPORATION, UTAH
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:HUNSTMAN CORPORATION;REEL/FRAME:007986/0353
Effective date: 19960129
|Aug 8, 1996||AS||Assignment|
Owner name: BANKERS TRUST COMPANY, ILLINOIS
Free format text: SECURITY AGREEMENT;ASSIGNOR:HUNTSMAN PETROCHEMICAL CORPORATION;REEL/FRAME:008067/0311
Effective date: 19960129
|Nov 6, 1996||AS||Assignment|
Owner name: BANKERS TRUST COMPANY, ILLINOIS
Free format text: SECURITY AGREEMENT;ASSIGNOR:HUNTSMAN PETROCHEMICAL CORPORATION;REEL/FRAME:008209/0244
Effective date: 19961023
Owner name: HUNTSMAN CORPORATION, UTAH
Free format text: RELEASE BY SECURED PARTY;ASSIGNOR:UNITED STATES TRUST COMPANY OF NEW YORK;REEL/FRAME:008209/0119
Effective date: 19960129
|Mar 31, 1998||REMI||Maintenance fee reminder mailed|
|Sep 6, 1998||LAPS||Lapse for failure to pay maintenance fees|
|Nov 17, 1998||FP||Expired due to failure to pay maintenance fee|
Effective date: 19980904